EP1814661A1 - Procede de regeneration d'un catalyseur - Google Patents

Procede de regeneration d'un catalyseur

Info

Publication number
EP1814661A1
EP1814661A1 EP05816031A EP05816031A EP1814661A1 EP 1814661 A1 EP1814661 A1 EP 1814661A1 EP 05816031 A EP05816031 A EP 05816031A EP 05816031 A EP05816031 A EP 05816031A EP 1814661 A1 EP1814661 A1 EP 1814661A1
Authority
EP
European Patent Office
Prior art keywords
catalyst
acid
platinum
regenerating
set forth
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP05816031A
Other languages
German (de)
English (en)
Inventor
Lee Rigby
R. Merritt Sink
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of EP1814661A1 publication Critical patent/EP1814661A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/082—Compounds containing nitrogen and non-metals and optionally metals
    • C01B21/14—Hydroxylamine; Salts thereof
    • C01B21/1409—Preparation
    • C01B21/1418—Preparation by catalytic reduction of nitrogen oxides or nitrates with hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/48—Liquid treating or treating in liquid phase, e.g. dissolved or suspended
    • B01J38/60—Liquid treating or treating in liquid phase, e.g. dissolved or suspended using acids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/90—Regeneration or reactivation
    • B01J23/96—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the noble metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/48—Liquid treating or treating in liquid phase, e.g. dissolved or suspended
    • B01J38/68—Liquid treating or treating in liquid phase, e.g. dissolved or suspended including substantial dissolution or chemical precipitation of a catalyst component in the ultimate reconstitution of the catalyst
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S502/00—Catalyst, solid sorbent, or support therefor: product or process of making
    • Y10S502/514—Process applicable either to preparing or to regenerating or to rehabilitating catalyst or sorbent

Definitions

  • the subject invention generally relates to a method of regenerating a catalyst and a method of preparing hydroxylammonium salts. More specifically, the subject invention relates to using ammonium sulfate in a preparation of the catalyst from an acid.
  • Catalysts are known in the art. Typically, catalysts are used in commercial processes in preparation of hydroxylammonium salts. A specific catalyst includes platinum applied on a carrier. If the platinum is applied on the carrier and used in manufacturing of hydroxylammonium salts, the catalyst may become at least partially poisoned with a metal. The metal is typically a transition metal such as mercury or copper. In rare occurrences, the catalyst may become extensively poisoned as a result of extensive impurities in raw materials used to make the hydroxylammonium salts. As a result of poisoning, the catalyst must be regenerated to remain effective. Methods of regenerating catalysts are also known in the art.
  • a first type of prior art method includes precipitation of the platinum from an acid with metallic or organic compounds.
  • a second type of prior art method includes precipitation of the metal that poisons the catalyst from an acid using organic compounds.
  • a third type of prior art method includes dissolving the platinum and the metal that poisons the catalyst in acid and subsequently precipitating the platinum onto the carrier.
  • the '540 patent further discloses selectively precipitating the platinum from the acid with hydrazine hydrate or metals such as aluminum, zinc, and magnesium. Yet, the '540 patent discloses that using the metals such as aluminum, zinc, and magnesium is undesirable when high purity of the platinum is required.
  • a readily available and relatively inexpensive non-metallic inorganic ammonium salt such as ammonium sulfate to precipitate the platinum.
  • the '540 patent does not disclose the use of ammonium sulfate or any plentiful by-product of a commercial process to precipitate the platinum. Therefore, the '540 patent does not disclose a cost efficient method of regenerating the catalyst using a non-metallic inorganic salt. Thus, the method disclosed in the '540 patent is not effective for use in commercial processes such as synthesis of caprolactam.
  • the '133 patent does not disclose precipitation of the platinum as an insoluble salt from the acid or use of ammonium sulfate to precipitate the platinum as an insoluble salt. Thus, the '133 patent does not disclose a cost efficient method for effectively separating the platinum from the metal that poisons the catalyst.
  • the '133 patent precipitates the platinum onto the carrier after dissolution in the acid, it is likely that the method disclosed in the '133 patent also precipitates the metal that poisons the catalyst back onto the carrier. Any precipitation of the metal that poisons the catalyst back onto the carrier would reduce the efficiency of the method. Therefore, the '133 patent does not disclose an effective separation of the platinum or a method that is effective for use in commercial processes such as synthesis of caprolactam and ammonium sulfate.
  • the prior art methods of regenerating catalysts, as described immediately above have not been optimized for cost efficiency in commercial processes. The prior art methods are not suitable for use in commercial processes for various reasons.
  • the subject invention provides a method of regenerating a catalyst having platinum applied on a carrier.
  • the catalyst is at least partially poisoned with a metal.
  • the catalyst becomes at least partially poisoned as a result of use in preparation of hydroxylammonium salts.
  • the method includes dissolving the platinum and the metal in a first acid.
  • the method also includes adding ammonium sulfate to the first acid to precipitate the platinum.
  • the method further includes precipitating the platinum onto the carrier for reuse.
  • the subject method also provides a method of preparing hydroxylammonium salts.
  • the catalyst which, as described above, has been regenerated by precipitation of the platinum with ammonium sulfate is used to prepare the hydroxylammonium salts.
  • the methods of regenerating the catalyst and preparing the hydroxylammonium salts are used to decrease industrial production costs. Specifically, the methods are most often used when extensive poisoning of the catalyst has occurred due to extensive impurities in raw materials used to create the hydroxylammonium salts, however the methods can be used whenever any poisoning has occurred.
  • the methods utilize ammonium sulfate, a plentiful by-product of caprolactam synthesis, to regenerate the catalyst for use in efficient production of hydroxylammonium salts, specifically, hydroxylamine.
  • the use of ammonium sulfate improves a time of regeneration of the catalyst and limits a loss of production of hydroxylamine due to poisoning of the catalyst, thus saving overall production costs due to a potential loss of caprolactam.
  • the methods of regenerating the catalyst and preparing hydroxylammonium salts, according to the present invention also yield additional advantages.
  • a first additional advantage includes reducing an amount of the metal that poisons the catalyst.
  • a second additional advantage includes reducing an amount of the platinum leftover in solution after precipitation of the platinum with ammonium sulfate.
  • a third additional advantage includes recovering the metal that poisons the catalyst from the filtrate and recovering any leftover platinum. This reduces an amount of waste transferred to the environment when a filtrate is discarded and when the platinum is reclaimed.
  • Figure 1 is a bar graph illustrating concentration of platinum on a catalyst using various ammonium sulfate regeneration procedures.
  • Figure 2 is a bar graph illustrating concentration of mercury and copper on a catalyst using various ammonium sulfate regeneration procedures.
  • Figure 3 is a bar graph illustrating concentration of platinum, mercury, and copper on a second carrier from an original filtrate.
  • a method of regenerating a catalyst having platinum applied on a carrier is provided and described additionally below.
  • the method of the present invention is used to improve manufacturing reliability and decrease industrial production costs associated with preparation of hydroxylammonium salts.
  • the method is typically utilized when extensive poisoning of the catalyst has occurred due to extensive impurities in raw materials used to create the hydroxylammonium salts, however the method can be used whenever any poisoning has occurred.
  • the method utilizes a plentiful by-product of a commercial process also described additionally below. Most preferably, the method regenerates the catalyst for use in efficient production of hydroxylamine. But, hydroxylamine can be produced via a variety of processes and methods.
  • hydroxylamine can be formed as a hydroxylammonium salt.
  • a method of preparing hydroxylammonium salts includes using the catalyst having platinum applied on the carrier that has been regenerated by precipitation of the platinum with ammonium sulfate.
  • the method of preparing hydroxylammonium salts may also include the step of reacting nitric oxide and hydrogen in the presence of the catalyst. If the nitric oxide is reacted with the hydrogen, the nitric oxide is preferably gaseous and preferably reacted in an amount of from 5.0 to 40.0, more preferably of from 15.0 to 40.0, and most preferably of from 25.0 to 35.0 percent by volume per 100 percent by volume. Also, if the nitric oxide is reacted with the hydrogen, the hydrogen is preferably gaseous and preferably reacted in an amount of from 10.0 to 80.0, more preferably of from 35.0 to 80.0, and most preferably of from 65.0 to 75.0 percent by volume per 100 percent by volume.
  • the method of preparing hydroxylamrnoniurn salts may also include the step of suspending the catalyst in a processing acid.
  • the processing acid includes, but is not limited to, a mineral acid. Most preferably, the processing acid includes sulfuric acid.
  • a method of preparing the caprolactam includes providing a catalyst that has been regenerated by precipitation of the platinum with ammonium sulfate. It is preferred that the catalyst is provided in an amount of from 10.0 to 60.0, more preferably from 10.0 to 40.0, and most preferably from 10.0 to 30.0 grams per one liter volume of a reactor. The method also includes forming hydroxylamine in the presence of the regenerated catalyst.
  • the catalyst is at least partially poisoned with a metal as a result of use in preparation of hydroxylammonium salts.
  • the carrier includes all possible acid-proof substances including, but not limited to, graphite, activated charcoal, and barium sulfate. In the commercial process associated with the present invention, graphite is especially useful and cost effective, and is most preferred. It is contemplated that the metal poisoning the catalyst may include, but is not limited to, mercury, copper, and combinations thereof.
  • the method includes dissolving the platinum, preferably slurried in water, and the metal in a first acid.
  • the first acid includes, but is not limited to, at least one mineral acid. More preferably, the first acid includes a combination of two acids including hydrochloric acid and nitric acid. Other options include, but are not limited to, sulfuric acid, chlorosulfuric acid, hydrobromic acid, hydriodic acid, hydrofluoric acid, perchloric acid, and combinations thereof. Most preferably, the first acid includes aqua regia. Aqua regia is defined as a combination of nitric acid and hydrochloric acid, usually in a volumetric ratio of 1 :3.
  • aqua regia dissolves the platinum and the metal that poisons the catalyst because, in combination, the nitric acid and the hydrochloric acid perform different functions.
  • the nitric acid a powerful oxidizer, dissolves a small amount of the platinum and the metal poisoning the catalyst thereby forming platinum ions and metal ions, respectively.
  • the hydrochloric acid provides chloride ions that react with the platinum ions and the metal ions. It is believed that reacting the platinum ions and the metal ions with the chloride ions allows further oxidation of the platinum and the metal to take place, thus increasing dissolution of the platinum and the metal.
  • the method of regenerating the catalyst may include the step of heating the first acid. If heating is conducted, it is preferred that the first acid is heated after dissolving the platinum and the metal in the first acid. If the first acid is heated, the first acid is
  • the method also optionally includes stirring the first acid. If stirring is conducted, it is preferred that stirring the first acid occurs as the first acid is heated. When stirred, the first acid is preferably stirred from 30 minutes to 3.50 hours and most preferably from 1.75 to 2.25 hours. [0025] If the first acid is heated, the first acid, now including the platinum and the metal, is preferably cooled. However, as described above, heating is optional so that cooling may not be necessary. If the first acid is cooled, the first acid is cooled preferably to
  • the method of regenerating the catalyst also includes adding ammonium sulfate to the first acid to precipitate the platinum as a sulfate salt. It is contemplated that other ammonium salts may also be used to precipitate the platinum as the sulfate salt. These other ammonium salts include ammonium nitrate, ammonium perchlorate, ammonium phosphate, and mixtures thereof.
  • the ammonium sulfate is preferably added in an amount of from 50 to 80, more preferably of from 60 to 75, and most preferably of from 65 to 70 parts by weight per 100 parts by weight of the catalyst. Without intending to be bound by theory, it is believed that ammonium ions form a coordinate bond with the platinum to form the sulfate salt.
  • the first acid may be stirred after the ammonium sulfate is added.
  • the first acid is stirred, it is preferred that the first acid is stirred from 30 minutes to 3.50 hours and most preferably from 1.75 to 2.25 hours. It is believed that stirring the first acid after the ammonium sulfate is added allows for greater precipitation of the platinum due to total mixing of ammonium sulfate and the first acid.
  • the method of regenerating the catalyst preferably includes separating the platinum precipitated with ammonium sulfate from the first acid and the metal dissolved in the first acid.
  • a technique to separate the platinum includes, but is not limited to, filtration. If filtering occurs, the platinum is separated from the metal as a retentate.
  • the metal dissolved in the first acid is a filtrate.
  • the filtrate may be reserved separately from the catalyst. Use of the filtrate is described additionally below.
  • the method of regenerating the catalyst may include adding additional ammonium sulfate to rinse the retentate on a filter bed. Preferably, any additional platinum that is precipitated remains on the retentate within the filter bed. It is believed that rinsing the catalyst removes any leftover metal and any acid while maintaining the platinum as the sulfate salt.
  • the method of regenerating the catalyst also includes optionally adding the platinum that has been precipitated with ammonium sulfate to water to form a suspension. If the platinum is added to the water to form a suspension, it is preferred that the platinum is added to the water after the platinum is separated from the first acid and the metal dissolved in the first acid.
  • the method of regenerating the catalyst may also include mixing the suspension. Without intending to be bound by theory, it is believed that mixing the suspension breaks up the platinum precipitated with ammonium sulfate and introduces the platinum into solution with the water.
  • the suspension may be heated under a nitrogen stream. If heating occurs under the nitrogen stream, it is preferred that the suspension is heated under the nitrogen stream after the catalyst is added to the water.
  • the suspension is preferably heated to from 60 to 100 0 C and most preferably to
  • the method of regenerating the catalyst also includes adding a base to the suspension. If the base is added to the suspension, it is preferred that the base is added to the suspension after the suspension has been heated under the nitrogen stream. If addition to the suspension results, the base preferably includes, but is not limited to, an alkaline metal salt. More preferably, the base includes an alkaline metal salt that is organic. Most preferably, the base includes sodium acetate. Adding the base to the suspension preferably raises a pH of the suspension to from 3.0 to 7.0 and most preferably to from 4.0 to 6.0.
  • the method of regenerating the catalyst includes adding a selective poisoning compound to the suspension.
  • the selective poisoning compound includes, but is not limited to, sulfur, sodium dithionite, and combinations thereof. Most preferably, the selective poisoning compound includes sulfur.
  • the selective poisoning compound is preferably added after the base is added to the suspension. Also if the selective poisoning compound is added to the suspension, it is preferably added in an amount of from 0.005 to 0.100, more preferably of from 0.010 to 0.050, and most preferably of from 0.020 to 0.040 parts by weight per 100 parts by weight of the platinum. It is believed that the selective poisoning compound is added to the suspension to intentionally selectively poison the catalyst.
  • the catalyst is poisoned with the selective poisoning compound to balance selectivity and yield of the catalyst.
  • An excess of the selective poisoning compound reduces the yield of the catalyst but allows the catalyst to be more highly selective.
  • a lack of the selective poisoning compound allows the catalyst to produce high yields but reduces the selectivity of the catalyst towards hydroxylamine.
  • the method of regenerating the catalyst also includes optionally cooling the suspension including the selective poisoning compound.
  • the suspension is cooled, it is preferred that the suspension is cooled to from 40 to 80 0 C
  • the method of regenerating the catalyst further includes precipitating the platinum onto the carrier for reuse.
  • the platinum may be precipitated onto the carrier for reuse through the addition of a second acid to the suspension.
  • the second acid includes, but is not limited to, an organic acid.
  • the second acid includes formic acid. It is believed that formic acid acts to reduce platinum from an oxidized state to a ground state, thereby causing the platinum to precipitate onto the carrier. Additionally, the selective poisoning compound would also precipitate onto the carrier.
  • the method of regenerating the catalyst also includes optionally stirring the suspension including the second acid.
  • the suspension is preferably stirred from 6 to 60 minutes and most preferably from 27 to 33 minutes.
  • the method of regenerating the catalyst includes heating the suspension including the second acid. If the suspension is heated, the suspension is preferably heated after the suspension is stirred. Also, if the suspension is heated, the
  • suspension is preferably heated to from 60 to 100 0 C and most preferably to from 80 to
  • the suspension including the second acid may be stirred a second time. If stirring occurs a second time, the suspension is preferably stirred after the suspension has been heated. Also, if the suspension is stirred for a second time, the suspension is preferably stirred from 1.0 to 5.0 hours and most preferably from 2.5 to 3.5 hours.
  • the suspension is preferably cooled. However, as described above, heating is optional so that cooling may not be necessary. If the suspension is cooled, the suspension is preferably cooled to from 30 to 70°C and most preferably to from 40 to 6O 0 C. Finally, the platinum precipitated onto the
  • the carrier may be separated from the suspension under the nitrogen stream and may be washed with water. It is believed that the nitrogen stream eliminates the possibility of forming oxides, such as PtO 2 , a possible contaminant of the catalyst. Also, it is believed that the water will wash away any loose impurities from the catalyst thereby increasing purity of the catalyst.
  • the method continues and allows the metal originally poisoning the platinum catalyst to be recovered.
  • the filtrate as described above, may be utilized to recover the metal originally poisoning the catalyst.
  • a second carrier which is the same as the first carrier, may be added to the filtrate in small quantities. Any dissolved metal in the filtrate originally poisoning the catalyst may be precipihtated onto the second carrier for recovery. If the second carrier is added, it is preferred that the second carrier is added in an amount of from 1.0 to 5.0, more preferably from 1.0 to 4.0, and most preferably from 1.5 to 3.0 parts by weight per 100 parts by weight of the filtrate.
  • the method of recovering the metal originally poisoning the catalyst may include stirring the filtrate under the nitrogen stream. If stirring under the nitrogen stream is conducted, it is preferred that the filtrate is stirred after the second carrier is added.
  • the method of recovering the metal originally poisoning the catalyst includes adding a base to the filtrate and the second carrier. If the base is added to the filtrate, the base is preferably added to the filtrate after the filtrate has been
  • the base includes sodium carbonate as the inorganic alkaline metal salt and sodium acetate as the organic alkaline metal salt. If both bases are utilized, it is preferred that sodium carbonate is added before the sodium acetate. If the sodium acetate is utilized, it is preferred that the sodium carbonate is added to the filtrate in an amount such that the pH of the filtrate is initially raised to from 0.5 to 3.0 and most preferably raised to from 1.4 to 1.6. Further, if the sodium acetate is utilized, it is preferred that the sodium acetate is added to the filtrate in amount such that the pH of the filtrate is additionally raised to from 3 to 7 and most preferably raised to from 4.0 to 6.0.
  • the method of recovering the metal originally poisoning the catalyst also includes optionally adding a third acid to the filtrate and the second carrier to reclaim any leftover platinum and recover any metal originally poisoning the catalyst.
  • the third acid is preferably added after the base is added to the filtrate.
  • the third acid includes, but is not limited to, an organic acid.
  • the third acid includes formic acid. If the third acid is added to the filtrate, it is preferred that the third acid is added to the filtrate in an amount of from 2.0 to 8.0, more preferably from 3.0 to 6.0, and most preferably from 3.0 to 5.0 parts by weight per 100 parts by weight of the total solution.
  • the method of recovering the metal originally poisoning the catalyst may also include heating the filtrate. If heating the filtrate occurs, the filtrate is preferably heated after the third acid is added to the filtrate. Also, if the filtrate is heated, the filtrate is
  • the filtrate may optionally be stirred. If stirring results, the filtrate is preferably stirred from 1.0 to 5.0 hours and most preferably from 2.5 to 3.5 hours. In other embodiments, the filtrate may be cooled, washed, and/or dried, preferably after heating the filtrate including the third acid.
  • a first advantage includes reducing a loss of the platinum on the carrier, as shown in Figure 1.
  • a second advantage includes reducing an amount of mercury and copper remaining on the catalyst after regeneration of the catalyst with ammonium sulfate, as shown in Figure 2.
  • a third advantage includes recovering the metal from the filtrate, as shown in Figure 3, to reduce an amount of waste transferred to the environment and to reclaim any remaining platinum.
  • the terminology “No treatment” indicates that the platinum was not subject to any experimental method change during catalyst regeneration.
  • the terminology “Ix ammonium sulfate” indicates that the platinum was dissolved in the first acid, ammonium sulfate was added in equal amounts to the platinum, and the pH of the first acid was not adjusted and was less than one.
  • the terminology “2x ammonium sulfate” indicates that the platinum was dissolved in the first acid, twice the amount of ammonium sulfate to the platinum was added in comparison to the Ix ammonium sulfate condition, and the pH of the first acid was not adjusted.

Abstract

Le procédé de l'invention consiste à appliquer du platine sur un support tel que le graphite de façon à former un catalyseur platine. Le catalyseur est empoisonné par un métal conséquemment à l'utilisation du catalyseur dans la préparation de sels d'hydroxyammonium. Un procédé de régénération du catalyseur consiste à dissoudre le platine et le métal dans un acide. Le procédé consiste également à ajouter du sulfate d'ammonium à l'acide pour précipiter le platine. Le sulfate d'ammonium est un sous-produit d'un procédé commercial de synthèse d'un caprolactame. Le procédé consiste également à précipiter le platine sur le support pour le réutiliser dans la préparation de sels d'hydroxyammonium et dans la préparation du caprolactame.
EP05816031A 2004-11-10 2005-11-10 Procede de regeneration d'un catalyseur Withdrawn EP1814661A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US98510304A 2004-11-10 2004-11-10
PCT/EP2005/012079 WO2006050962A1 (fr) 2004-11-10 2005-11-10 Procede de regeneration d'un catalyseur

Publications (1)

Publication Number Publication Date
EP1814661A1 true EP1814661A1 (fr) 2007-08-08

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP05816031A Withdrawn EP1814661A1 (fr) 2004-11-10 2005-11-10 Procede de regeneration d'un catalyseur

Country Status (11)

Country Link
US (1) US7811955B2 (fr)
EP (1) EP1814661A1 (fr)
JP (1) JP4976306B2 (fr)
KR (1) KR20070085949A (fr)
CN (1) CN101056705B (fr)
AU (1) AU2005303890A1 (fr)
BR (1) BRPI0517614A (fr)
CA (1) CA2584802A1 (fr)
MX (1) MX2007005042A (fr)
RU (1) RU2007121512A (fr)
WO (1) WO2006050962A1 (fr)

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Publication number Priority date Publication date Assignee Title
UA95907C2 (en) * 2005-05-02 2011-09-26 Эррей Биофарма Инк. Mitotic kinesin inhibitors and methods of use thereof
PL1977995T3 (pl) * 2007-04-05 2012-04-30 China Petrochemical Dev Corporation Sposób wytwarzania hydroksyloaminy
DE102008012227A1 (de) * 2008-03-03 2009-09-17 Basf Se Regenerierung von Hydrierungskatalysatoren auf der Basis eines Platinmetalls
US8216532B1 (en) 2011-06-17 2012-07-10 Vierheilig Albert A Methods of recovering rare earth elements
CN116060425B (zh) * 2023-03-08 2023-06-02 国能龙源环保有限公司 一种脱除废弃脱硝催化剂表面Hg的方法

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Publication number Priority date Publication date Assignee Title
US2787540A (en) 1949-12-22 1957-04-02 Universal Oil Prod Co Recovery of platinum
CH395038A (de) * 1960-03-11 1965-07-15 Basf Ag Verfahren zur Herstellung von Platin-Träger-Katalysatoren für die Synthese von Hydroxylamin aus Stickoxyd und Wasserstoff
GB1197619A (en) * 1967-11-15 1970-07-08 Zaklady Azotowe Im Pawla Finde Method of Preparing and Regenerating an Active and Selective Catalyst for the Production of Hydroxylamine Salt.
CH585581A5 (fr) * 1974-03-21 1977-03-15 Inventa Ag
DE3507832A1 (de) * 1985-03-06 1986-09-11 Basf Ag, 6700 Ludwigshafen Verfahren zur regenerierung von inaktiven und vergifteten platinkatalysatoren
DE19618829A1 (de) * 1996-05-10 1997-11-13 Bayer Ag Verfahren zur Reaktivierung von Platinmetall enthaltenden Katalysatorsystemen

Non-Patent Citations (1)

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Title
See references of WO2006050962A1 *

Also Published As

Publication number Publication date
MX2007005042A (es) 2007-06-19
CA2584802A1 (fr) 2006-05-18
RU2007121512A (ru) 2008-12-20
US20070293389A1 (en) 2007-12-20
US7811955B2 (en) 2010-10-12
AU2005303890A1 (en) 2006-05-18
CN101056705A (zh) 2007-10-17
WO2006050962A1 (fr) 2006-05-18
JP2008519682A (ja) 2008-06-12
JP4976306B2 (ja) 2012-07-18
CN101056705B (zh) 2011-11-09
BRPI0517614A (pt) 2008-10-14
KR20070085949A (ko) 2007-08-27

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